Separation of hydrocarbons water/emulsifier mixtures

Abstract

A process for separating vaporous mixtures of hydrocarbons, water and emulsifier derived from the remediation of wellbore fluid, such as a mud containing solid particulate material in which the vaporous mixture is quenched with a hydrocarbon stream which is at a temperature above the boiling point of water and below the boiling point of the hydrocarbons in the vaporous stream. Most of the hydrocarbons in the vaporous stream and substantially all of the emulsifier are condensed into the hydrocarbon quench to form an oil stream. The water is recovered from the hydrocarbon quench as a vaporous stream and quenched with water. The quenched water and any residual heavier hydrocarbons are separated by phase separation.

Description

BACKGROUND OF THE INVENTION

1. Field of the Invention

The present invention relates to apparatus and a method of separating hydrocarbons from mixtures with water, in particular hydrocarbon/water/emulsifier mixtures recovered from wellbore fluids in remediation processes.

2. Related Information

Due to environmental concerns the removal of volatile material from solids has become an important process. Far example, volatile materials must be removed from solids in the reclamation of petroleum lubricated drilling fluids used in the exploration and production of petroleum oils. The drilling fluid, referred to as "mud", serves several purposes, the most important of which includes cooling and lubricating the bit and removing drilled solids, or cuttings, from the borehole. While most mud is a water based, flowable composition, the drilling mud is frequently compounded with a lubricant material such as diesel, crude oil or other non-water petroleum based constituent and various surfactants or emulsifiers to create stable emulsions of the water and hydrocarbon to facilitate the mud's lubricating characteristics.

The mud may be contained in a mud tank, which is connected by way of a mud line and mud pump to a hose and swivel used to inject the mud into the tap of the drill pipe. The returning mud, combined with the cuttings, is captured in a mud return pipe and recirculated through the drill pipe.

When the concentration of the drill cuttings in the mud rises too high recirculation of the mud becomes a problem. In order for the mud to perform its several functions, its viscosity, density and other properties must be maintained within acceptable limits. The drill cuttings adversely affect these properties thus reducing the carrying capacity of the mud and damaging the drilling equipment.

To allow for effective recirculation, the mud is usually separated from the cuttings prior to being recycled through the drill string. The cuttings are then disposed of as waste which presents a problem when the lubricating properties of the mud have been enhanced by the addition of hydrocarbons. Because of the hydrocarbons in the cuttings a hazardous waste problem is presented. Historically, the contaminated cuttings were diluted by mixing and hauled to remote sites for disposal in landfills. This, however, also presents a problem in that the landfill then becomes a "hazardous" waste site leaving the dumper liable for environmental damages indefinitely.

Decontaminating the cuttings is more attractive. Treatment processes heretofore available to remove oil or other hydrocarbons from cuttings include distillation, solvent washing, and mud burning. While these processes are effective to varying degrees at stripping the hydrocarbon contaminants from cuttings, rendering the cuttings environmentally clean, they remain problematic in that disposal persists with the liquid or vapor from the disassociated contaminant.

There are several patents on rotary kilns specifically designed to remove volatile hydrocarbons from solid material such as soil. See for example U.S. Pat. Nos. 5,152,233; 5,199,354; 5,302,118; and 5,378,059. All of the rotary kilns are gas fired with the hot combustion gases being directed into the drum to heat the solids. When the solids have a substantial quantity of hydrocarbonaceous material an explosion hazard may be present. In addition, when the flame is applied directly to the contaminated materials, the solids are burned so that the contaminants are consumed and turned into smoke which may be an environmental hazard.

In order to achieve remediation, it has been determined that the hydrocarbons and water extracted with the cuttings from the wellbore fluid must be separated to recycle the materials or recover them for other disposition. One would normally expect that phase separation of the water and oil would be easily accomplished. However, when hydrocarbons such as diesel are incorporated in the water, surfactants or other emulsifiers must be added to obtain stable emulsion of the water/oil mixtures during use in the wellbore. These emulsifiers are volatilized out of the kiln along with the water and hydrocarbons, resulting in a recovered material, which when condensed is again a stable emulsion of water and oil.

One feature of this invention is to provide an apparatus to receive volatile contaminants from solids to recover and/or recycle the disassociated hydrocarbons. It is a particular feature that the present invention provides a process to separate water from hydrocarbons without the formation of stable emulsions thereof.

SUMMARY OF THE INVENTION

The invention concerns a process for obtaining separation of a mixed vaporous stream comprising hydrocarbons, water and emulsifier comprising:

contacting a first vaporous stream comprising hydrocarbons, water and emulsifier with a quench hydrocarbon stream, said quench hydrocarbon stream being at a temperature above the boiling point of water and below the boiling point of the hydrocarbon in said first vaporous stream, to condense a major portion of the hydrocarbon in said first vaporous stream and substantially all of said emulsifier to form an oil stream;

recovering a second vaporous stream comprising substantially all of the water as vapor;

condensing said water vapor and a minor portion of the hydrocarbons in said second vaporous stream and

separating said condensed water and hydrocarbons by phase separation.

Optimizing the process conditions can result in recovering over 98% of the hydrocarbon (organic compounds) in the vapor from the kiln.

A suitable quench hydrocarbon would include hydrocarbons such as diesel fuel which may correspond to the hydrocarbons in the wellbore fluid, however, any hydrocarbon which is a flowable liquid under the conditions of the process may be used.

It should be appreciated that the present apparatus and process are useful for any soil type remediation, especially where the water and hydrocarbons (including modified hydrocarbons which may include other molecules than hydrogen and carbon, such as oxygen, sulfur, nitrogen, metals and the like), i.e. organic compounds, are volatilized under the conditions of the kiln.

The term emulsifier is used to include any compound organic or inorganic that would tend to make stable emulsions of water and oil, e.g., anionic and non ionic surfactants.

BRIEF DESCRIPTION OF THE DRAWING

The FIGURE is a simplified schematic representation of a preferred embodiment of the apparatus of the present invention for carrying out the process of the present invention.

DETAILED DESCRIPTION

A preferred kiln is essentially a unit which is a trailer mounted rotating drum through which contaminated soil, such as drilling cuttings, is heated and processed to remove and reclaim the contaminants. The contaminant is typically diesel oil which has been added to drilling muds. The soil which exits the unit is essentially contaminant free, and the diesel oil which has been vaporized during the heating process is condensed and collected.

The contaminated soil enters the unit through a hopper and is then propelled by means of an auger into the heated, rotating drum. Heat is applied to the outside of the rotating drum by means of two gas burners mounted on the bottom of the trailer. The flames, therefore, do not come in direct contact with the soil, with the heat being applied to the soil indirectly by conduction through the drum wall. For this process the soil temperatures must be in the 500°-900° F. range.

The burners are mounted in separate fireboxes aligned in tandem with the drum axis and are located far enough from the drum so that the flame does not impinge upon the drum. The drum is heated by radiation from the burner flames as well as from convection of air heated by the burner flames. Rotation of the drum prevents the burners from locally overheating the drum.

A stationary shroud, or heat jacket, encompasses the rotating drum and burners. Soil transit through the drum is regulated by drum rotation and inclination and feed rate. The drum is tilted slightly toward the exit end by lowering that end of the trailer.

Decontaminated soil exits the lower end of the drum through a double door arrangement which reduces dust from exiting and prevents air from entering the drum. A dust shroud encloses the double door exit end of the drum.

The oil vapors inside the drum are drawn out by applying a slight vacuum to the feed end of the drum. The withdrawn vapors are then sent to a condensing unit and collected. A more detailed description of the kiln is presented in U.S. patent application Ser. No. 08/796,086, filed Feb. 5, 1997 which is incorporated herein in its entirety.

In the FIGURE, line 10 carries kiln vapors comprising hydrocarbons, water, emulsifier and other volatile constituents from kiln 1. Line 12 carries cool oil quench which is sprayed into transfer line 14 carrying the kiln vapors to cool the kiln vapors and condense the major portion of the hydrocarbons. The condensed vapors are collected in primary separator 16 where the liquid hydrocarbon is separated via line 18a from water vapor and light hydrocarbons, such as methane and non-condensibles such as CO and CO₂ which exit the separator via line 20a.

In this first separation, not only are most of the hydrocarbons and water separated but the surfactants and emulsifiers which were added to the wellbore fluid are stripped into the liquid hydrocarbon fraction. Thus, the small amount of hydrocarbons remaining in the vaporous water phase is easily separated by phase separation since there is substantially none of the surfactant or emulsifier carried out in the vapor phase from primary separator 16.

The hydrocarbon (oil phase) recovered via line 18a is sent to filter 34 through pump 19 and line 18b. The filter may be, for example, an oil cyclone where dirty oil blowdown is collected via line 36 and recycled to the auger feed (not shown) to kiln 1 or otherwise disposed of.

The clean oil recovered via line 38 is cooled by an air cooled heat exchanger 40 exiting through line 42a. A portion may be sent to storage via line 42b and a portion sent through line 12 to quench the kiln vapors in line 14.

Cool water is sprayed from line 22b into transfer line 20 to condense out most of the water and some higher hydrocarbons, which is collected by secondary separator 24 where the condensed water and some hydrocarbons are recovered via line 26a. The non-condensibles, depending on the composition and the relevant environmental considerations, are recovered via line 28 and may be used as auxiliary fuel for the kiln burners 2.

The condensed material (mainly water) leaves secondary separator 24 via line 26a and is pumped by pump 27 through line 26b to air cooled heat exchanger 32 hence into line 46a. A portion of the material in line 46a is returned via line 44 to transfer line 20a to aid in cooling the vaporous feed from the primary separator 16. Also in this embodiment cooled material from secondary separator 24 via line 22a, pump 23 and line 22b is used to cool the incoming vapors in line 20a.

A portion of cooled condensed material from heat exchanger 32 is also sent to oil/water phase separator 48 via 46a where water is recovered from the bottom of separator 48 via line 50 and may be used as dust suppressor spray 52 in the kiln or kiln product (not shown) or recovered for disposal via line 54.

The hydrocarbon phase from separator 48 is recovered and sent to storage via 56 and 42c.

In the schematic FIGURE many of the pumps, valves, pressure regulators and other items of conventional equipment are omitted, however their use and placement are readily apparent to those of ordinary skill.

In the TABLE data for a typical operation of a vapor recovery unit operating in accordance with the preferred embodiment is presented.

TABLE
__________________________________________________________________________
STREAM NO.
14  20a 18a 18b 42a 42b
12  20b 22a
__________________________________________________________________________
TEMP. °F.
249 249 249 249 125 125
125 148 148
PRESS. PSIA
14  14  14  90  75  75 75  13  13
FLOW, #/HR
15,372
2,035
13,337
13,337
13,337
1,337
12,000
52,035
358
__________________________________________________________________________
STREAM NO.
26a 26b 46a 22b 44  46b
56  54  42c
50
__________________________________________________________________________
TEMP. °F.
148 148 115 203 115 115
115 115 123
115
PRESS. PSIA
13  90  75  17  75  75 75  75  75 75
FLOW, #/HR
51,667
51,667
51,667
358 50,000
1,677
242 435 1,579
1,000
__________________________________________________________________________

Claims

1. A process for obtaining separation of a mixed vaporous stream comprising hydrocarbons, water and emulsifier comprising:

contacting a first vaporous stream comprising hydrocarbons, water and emulsifier with a quench hydrocarbon stream, said quench hydrocarbon stream being at a temperature above the boiling point of water and below the boiling point of the hydrocarbon in said first vaporous stream, to condense a portion of the hydrocarbon in said first vaporous stream and substantially all of said emulsifier to form an oil stream;

recovering a second vaporous stream comprising substantially all of the water as vapor;

condensing said water vapor and a portion of the hydrocarbons in said second vaporous stream and

separating said condensed water and hydrocarbons by phase separation.

2. The process according to claim 1 comprising quenching said second vaporous stream with water.

3. The process according to claim 1 wherein said oil stream is filtered to remove contaminants and a purified oil stream and a dirty oil stream recovered.

4. The process according to claim 3 wherein said purified oil stream is cooled and a portion recycled to contact said first vaporous stream.

5. The process according to claim 3 wherein said first vaporous stream is produced from wellbore fluid and said dirty oil stream is returned to said wellbore fluid.

6. The process according to claim 2 comprising cooling a portion of said condensed water and quenching said second vaporous stream therewith.

7. The process according to claim 1 wherein said hydrocarbons separated from the second vaporous stream are combined with a portion of said purified oil.

8. The process according to claim 1 comprising suppressing dust in a kiln with a portion of the water separated from the second vaporous stream.

9. The process according to claim 3 wherein a portion of said purified oil is recovered.

10. The process according to claim 1 wherein non condensible gas is separated from said second vaporous stream.

11. The process according to claim 10 comprising firing a kiln with a portion of said non condensible gas.

12. The process according to claim 2 wherein said oil stream is filtered to remove contaminants and a purified oil stream and a dirty oil stream recovered.

13. The process according to claim 12 wherein said purified oil stream is cooled and a portion recycled to contact said first vaporous stream.

14. The process according to claim 13 wherein said first vaporous stream is produced from wellbore fluid and said dirty oil stream is returned to said wellbore fluid.

15. The process according to claim 14 comprising cooling a portion of said condensed water and quenching said second vaporous stream therewith.

16. The process according to claim 15 comprising suppressing dust in a kiln with a portion of the water separated from the second vaporous stream.

17. The process according to claim 16 wherein non condensible gas is separated from said second vaporous stream.

18. The process according to claim 17 comprising firing a kiln with a portion of said non condensible gas.